Shipborne three-phase separation and recycling system and method

Abstract

The invention relates to the field of mixture three-phase separation, and provides a shipborne three-phase separation recycling system and method.The system comprises the steps that a horizontal spiral centrifugal machine conducts three-phase separation on a fed euphausia superba solid-liquid mixture, and a first solid-phase output matter, a first liquid-phase output matter and a first oil-phase output matter are obtained; the disc centrifuge performs three-phase separation on the first liquid phase output substance and a third liquid phase output substance from the extruder to obtain a second solid phase output substance, a second liquid phase output substance and a second oil phase output substance, wherein the second solid phase output substance, the second liquid phase output substance and the second oil phase output substance are obtained from the second oil phase output substance; the first solid-phase output matter and the second solid-phase output matter are compressed, sheared and dewatered by the extruding machine, and a target euphausia superba solid matter and a third liquid-phase output matter are obtained; the heat exchange flocculation assembly is used for heating, flocculating and filtering the second liquid phase output substance to obtain the target protein phospholipid complex. The target protein phospholipid complex is obtained by fully utilizing the liquid-phase output substance, and the utilization rate is increased.

Description

TECHNICAL FIELD

[0001] The present application relates to the field of three-phase separation of mixtures, in particular to a shipborne three-phase separation recycling system and method. BACKGROUND

[0002] Antarctic krill, as one of the most abundant multicellular organisms on earth, is rich in protein, Omega-3 fatty acids, astaxanthin and other high-value components, and has extremely high commercial development potential. In the field of Antarctic krill resource development, the treatment method of the solid-liquid mixture after cooking Antarctic krill is relatively simple. In shipborne processing, the first three-phase separation is carried out by a horizontal screw centrifuge, the liquid output is output by a disc centrifuge for secondary three-phase separation, and the liquid obtained by the secondary three-phase separation is directly discharged into the sea. The solid output of the first three-phase separation and the solid output of the secondary three-phase separation are directly collected into a drying device. This scheme directly discharges the liquid output into the sea, cannot recover the water-soluble protein in the solid-liquid mixture, has low recycling rate, and the solid output directly enters the drying device, the water content is high, and it is easy to caking, which affects the drying effect.

[0003] In summary, at present, there is a lack of a system specially suitable for shipborne environment, high efficiency and capable of realizing precise three-phase (solid, liquid and oil) separation and protein phospholipid compound recycling for the solid-liquid mixture after cooking Antarctic krill. SUMMARY

[0004] The present application provides a shipborne three-phase separation recycling system and method, which solves the problem of low recycling rate in the prior art that the solid-liquid mixture after cooking Antarctic krill is directly subjected to three-phase separation, and the liquid output is discharged into the sea.

[0005] The shipborne three-phase separation recycling system and method provided by the present application adopt the following technical scheme:

[0006] A shipborne three-phase separation recycling system for the solid-liquid mixture of Antarctic krill separated and obtained after cooking, the system comprising a horizontal screw centrifuge, a disc centrifuge, an extruder and a heat exchange flocculation assembly;

[0007] The horizontal screw centrifuge separates the Antarctic krill solid-liquid mixture into a first solid phase output, a first liquid phase output and a first oil phase output;

[0008] The disc centrifuge is connected with the horizontal screw centrifuge, the extruder and the heat exchange flocculation assembly, and separates the first liquid phase output and the third liquid phase output from the extruder into a second solid phase output, a second liquid phase output and a second oil phase output;

[0009] The extruder is connected with the horizontal screw centrifuge and the disc centrifuge, and the first solid-phase output and the second solid-phase output are subjected to compression shear dewatering treatment to obtain target Antarctic krill solid and a third liquid-phase output;

[0010] The heat exchange flocculation assembly is connected with the disc centrifuge, and the second liquid-phase output is subjected to heating, flocculation and filtration to obtain the target protein phospholipid complex.

[0011] Optionally, the heat exchange flocculation assembly comprises a heat exchanger, a filter and at least one flocculation tank.

[0012] The heat exchanger is connected with the disc centrifuge, and the second liquid-phase output is subjected to internal heating to meet the target protein coagulation temperature condition.

[0013] The at least one flocculation tank is connected with the heat exchanger, and the heated second liquid-phase output is subjected to uniform flocculation treatment to obtain flocculation slurry.

[0014] The filter is connected with the at least one flocculation tank, and the flocculation slurry is subjected to separation to extract the target protein phospholipid complex.

[0015] Optionally, the system further comprises an output pump connected with the extruder to transport the target Antarctic krill solid.

[0016] Optionally, the horizontal screw centrifuge has a first feed inlet, a first solid-phase output port, a first liquid-phase output port and a first oil-phase output port, the disc centrifuge has a second feed inlet, a second solid-phase output port, a second liquid-phase output port and a second oil-phase output port, and the extruder has a third feed inlet, a third solid-phase output port and a third liquid-phase output port.

[0017] The first feed inlet is used for feeding the Antarctic krill solid-liquid mixture, the first solid-phase output port and the second solid-phase output port are both connected with the third feed inlet to transport the first solid-phase output and the second solid-phase output, the second liquid-phase output port and the third liquid-phase output port are both connected with the second feed inlet to transport the first liquid-phase output and the third liquid-phase output, and the first oil-phase output port is used for outputting the first oil-phase output; the second liquid-phase output port is connected with the heat exchange flocculation assembly to transport the second liquid-phase output, and the second oil-phase output port is used for outputting the second oil-phase output; and the third solid-phase output port is used for outputting the target Antarctic krill solid.

[0018] Optionally, the rotational speed of the horizontal screw centrifuge is 4500 rpm, the rotational speed of the disc centrifuge is 10000 rpm, the extruder is a double-screw extruder, the mesh size of the double-screw extruder is 0.5-1.0 mm, the compression ratio of the double-screw extruder is 6:1, and the rotational speed of the double-screw extruder is 100 rpm.

[0019] Optionally, the heat exchanger is a scraper heat exchanger, the PH value of the solution in the flocculation tank is 4.0-4.5, the solution in the flocculation tank is placed for 1.5-2.0 hours before the flocculation tank works, the filter is a horizontal microfilter, the screen aperture of the horizontal microfilter is 100 μm, and the rotating drum speed of the horizontal microfilter is 15-20 rpm.

[0020] Optionally, the heat exchanger is a scraper heat exchanger, the PH value of the solution in the flocculation tank is 4.0-4.5, the solution in the flocculation tank is placed for 1.5-2.0 hours before the flocculation tank works, the filter is a horizontal microfilter, the screen aperture of the horizontal microfilter is 100 μm, and the rotating drum speed of the horizontal microfilter is 15-20 rpm.

[0021] Optionally, the flocculation tank comprises a temperature sensor, a PH sensor, and a liquid passage pipeline arranged outside the cylinder wall, the temperature sensor is used to detect the temperature of the solution, the PH sensor is used to detect the PH value of the solution, and the liquid passage pipeline is used to pass in cooling water or hot water to realize temperature adjustment of the medium in the flocculation tank through wall heat conduction.

[0022] A shipborne three-phase separation recycling method based on the shipborne three-phase separation recycling system described above, the method comprising:

[0023] The Antarctic krill solid-liquid mixture obtained after the feed is cooked and separated;

[0024] The Antarctic krill solid-liquid mixture is subjected to three-phase separation to obtain a first solid-phase output, a first liquid-phase output, and a first oil-phase output;

[0025] The first liquid-phase output and the third liquid-phase output are subjected to three-phase separation to obtain a second solid-phase output and a second liquid-phase output; the third liquid-phase output is generated when the first solid-phase output and the second solid-phase output are subjected to compression shear dehydration treatment to obtain the target Antarctic krill solid material;

[0026] The second liquid-phase output is subjected to heating, flocculation, and filtration to obtain the target protein phospholipid complex.

[0027] Optionally, the heating, flocculation, and filtration of the second liquid-phase output to obtain the target protein phospholipid complex comprise:

[0028] The PH value of the second liquid-phase output is adjusted to be within the range of 4.0-4.5, and the second liquid-phase output is heated to 80-85℃;

[0029] According to the heat preservation time of 20 minutes, the temperature of the second liquid-phase output is maintained at 80-85℃;

[0030] The temperature of the second liquid phase output is reduced to 60℃ within 5 minutes, and the temperature of the second liquid phase output is maintained at 60℃ for 30 minutes according to the temperature reduction time, so as to promote the flocculation network of the flocculation in the second liquid phase output to expand;

[0031] The temperature of the second liquid phase output is continuously reduced to 45℃ within 5 minutes, and the temperature of the second liquid phase output is maintained at 45℃ for 30 minutes according to the promotion time, so as to promote the compaction of the flocculation and form the flocculation slurry;

[0032] The flocculation slurry is separated to extract the target protein phospholipid complex.

[0033] The present application includes at least one of the following beneficial technical effects:

[0034] 1. The first solid phase output of the horizontal screw centrifuge and the second solid phase output of the disc centrifuge are both obtained by extruding through an extruder, and the first liquid phase output of the horizontal screw centrifuge is subjected to secondary three-phase separation, so as to ensure that the target Euphausia superba solid product with low water content is generated, which on the one hand avoids the target Euphausia superba solid product with high water content from entering the subsequent Euphausia superba drying machine again to cause the caking of the dried material, and on the other hand improves the utilization rate.

[0035] 2. The first liquid phase output of the horizontal screw centrifuge and the third liquid phase output of the extruder are subjected to three-phase separation through a disc centrifuge to generate a second liquid phase output, and then heating, flocculation and filtration are performed to obtain the target protein phospholipid complex, so as to fully utilize the liquid phase output and ensure that the target protein phospholipid complex is generated with high utilization rate. The vacuum pulse flocculation technology is used to dynamically control the vacuum degree, frequency and time in stages, so as to synergistically strengthen the flocculation efficiency, protect the structure of the flocculation, and optimize the energy consumption.

[0036] 3. According to the present application, the target protein phospholipid complex, the target Euphausia superba solid product and the target Euphausia superba oil are obtained from the cooked Euphausia superba solid-liquid mixture, and the utilization rate is higher than that of the target Euphausia superba solid product and the target Euphausia superba oil. BRIEF DESCRIPTION OF DRAWINGS

[0037] Figure 1 is a block diagram of a shipborne three-phase separation recycling system provided by an embodiment of the present application.

[0038] Figure 2 is Figure 1 is a structural schematic diagram of a horizontal screw centrifuge, a disc centrifuge and an extruder in the present application.

[0039] Figure 3 is Figure 1 is a block diagram of a heat exchange and flocculation assembly in the present application.

[0040] Figure 4 is Figure 3A structure diagram of a heat exchange flocculation assembly.

[0041] Figure 5 A structure diagram of a shipborne three-phase separation recycling system.

[0042] Figure 6 A flow chart of a shipborne three-phase separation recycling method provided by an embodiment of the present application.

[0043] Legend: horizontal screw centrifuge 1, disc centrifuge 2, extruder 3, first feeding port 11, first solid phase output port 12, first liquid phase output port 14, first oil phase output port 13, second feeding port 21, second liquid phase output port 22, second oil phase output port 23, second solid phase output port 24, third feeding port 31, third solid phase output port 32, third liquid phase output port 33, output pump 4, output feeding port 41, output discharging port 42, heat exchanger 5, heat exchange feeding port 51, heat exchange output port 52, flocculation tank 6, flocculation feeding port 61, flocculation output port 62, filter 7, filter feeding port 71, first filter output port 72, second filter output port 73. DETAILED DESCRIPTION

[0044] The application will be further described below in conjunction with the drawings. It should be understood that the specific embodiments described herein are merely intended to explain the present application and are not intended to limit the present application.

[0045] In the following description, for the purposes of explanation, numerous specific details are set forth in order to provide a thorough understanding of the inventive concept. As part of the description, some of the diagrams in the present disclosure represent structures and devices in block diagram form in order to avoid obscuring the principles of the disclosed principles. Not all features of an actual implementation are necessarily described or implied. References in the present disclosure to "one implementation" or "an implementation" mean that a particular feature, structure, or characteristic described is included in at least one implementation, and multiple references to "one implementation" or "an implementation" do not necessarily all refer to the same implementation.

[0046] The terms "a," "an," and "the" are not intended to refer to singular entities, but include the general class of which a specific example can be used for illustration. The use of the terms "a" or "an" can mean any number of including "one," "one or more," "at least one," and "one or more than one." The term "or" means any one of the alternatives, as well as any combination of the alternatives, including all of the alternatives, unless the alternatives are expressly indicated to be mutually exclusive. The phrase "at least one of" in combination with a list of items is intended to refer to a single item from the list of items, or any combination of items from the list of items. The phrase does not require all of the listed items to be present.

[0047] One embodiment of the present application discloses a shipboard three-phase separation recycling system for processing Antarctic krill solid-liquid mixture obtained after cooking and separation. The system refers to the block diagram of Figure 1 , including a decanter centrifuge 1, a disc centrifuge 2, an extruder 3, and a heat exchange flocculation assembly.

[0048] The decanter centrifuge 1 performs three-phase separation on the feed of Antarctic krill solid-liquid mixture to obtain a first solid phase output, a first liquid phase output, and a first oil phase output; the disc centrifuge 2 is connected with the decanter centrifuge 1, the extruder 3, and the heat exchange flocculation assembly, and the disc centrifuge 2 performs three-phase separation on the first liquid phase output and a third liquid phase output from the extruder 3 to obtain a second solid phase output, a second liquid phase output, and a second oil phase output; the extruder 3 is connected with the decanter centrifuge 1 and the disc centrifuge 2, and performs compression shear dewatering treatment on the first solid phase output and the second solid phase output to obtain target Antarctic krill solid and the third liquid phase output; the heat exchange flocculation assembly is connected with the disc centrifuge 2, and performs heating, flocculation, and filtration on the second liquid phase output to obtain a target protein phospholipid complex.

[0049] Referring specifically to Figure 2 , the decanter centrifuge 1 has a first feed port 11, a first solid phase output port 12, a first liquid phase output port 14, and a first oil phase output port 13, the disc centrifuge 2 has a second feed port 21, a second solid phase output port 24, a second liquid phase output port 22, and a second oil phase output port 23, and the extruder 3 has a third feed port 31, a third solid phase output port 32, and a third liquid phase output port 33.

[0050] The first feeding port 11 is used for feeding the Euphausia Superba solid-liquid mixture, the first solid phase output port 12 and the second solid phase output port 24 are connected with the third feeding port 31 to transport the first solid phase output and the second solid phase output, the second liquid phase output port 22 and the third liquid phase output port 33 are connected with the second feeding port 21 to transport the first liquid phase output and the third liquid phase output, and the first oil phase output port 13 is used for outputting the first oil phase output; the second liquid phase output port 22 is connected with the heat exchange flocculation assembly to transport the second liquid phase output, the second oil phase output port 23 is used for outputting the second oil phase output, and the third solid phase output port 32 is used for outputting the target Euphausia Superba solid.

[0051] In one example, the rotation speed of the decanter centrifuge 1 is 4500 rpm, the rotation speed of the disc centrifuge 2 is 10000 rpm, the extruder 3 is a double screw extruder, the filter screen aperture of the double screw extruder is 0.5-1.0 mm, the compression ratio of the double screw extruder is 6:1, and the rotation speed of the double screw extruder is 100 rpm.

[0052] In one example, continuing to refer to Figure 1 As shown, the system further comprises an output pump 4 connected with the extruder 3 to transport the target Euphausia Superba solid. The output pump 4 is preferably a single screw pump.

[0053] For details, please continue to refer to Figure 2 As shown, the output pump 4 has an output feeding port 41 connected with the third solid phase output port 32 and an output discharging port 42 as an output port of the whole system. The output pump 4 is used for transporting the target Euphausia Superba solid.

[0054] In one example, referring to Figure 3 As shown, the heat exchange flocculation assembly comprises a heat exchanger 5, a filter 7 and at least one flocculation tank 6. The heat exchanger 5 is connected with the disc centrifuge 2 to internally heat the second liquid phase output to meet the target protein coagulation temperature condition; the at least one flocculation tank 6 is connected with the heat exchanger 5 to uniformly flocculate the heated second liquid phase output to obtain flocculation slurry; and the filter 7 is connected with the at least one flocculation tank 6 to separate the flocculation slurry to extract the target protein phospholipid complex.

[0055] For details, please refer to Figure 4 and Figure 5As shown, the heat exchanger 5 has a heat exchange inlet 51 and a heat exchange outlet 52, the flocculation tank 6 has a flocculation inlet 61 and a flocculation outlet 62, and the filter 7 has a filter inlet 71, a first filter outlet 72 and a second filter outlet 73. The heat exchange inlet 51 is connected to the second liquid phase outlet 22, the heat exchange outlet 52 is connected to all the flocculation inlets 61, all the flocculation outlets 62 are connected to the filter inlet 71, the first filter outlet 72 is used to output the target protein phospholipid complex, and the second filter outlet 73 is used to output water.

[0056] When there is only one flocculation tank 6, the flocculation tank 6 always works when the system is started. When there are multiple flocculation tanks 6, the flocculation tanks 6 can be started at intervals, i.e., only one flocculation tank 6 works at a time, or multiple flocculation tanks 6 can work at the same time.

[0057] In one example, the heat exchanger 5 is a scraped surface heat exchanger, the heat exchange inlet of the scraped surface heat exchanger is provided with a pH regulator, the pH regulator adjusts the pH value of the second liquid phase output injected into the scraped surface heat exchanger to 4.0-4.5 by injecting a pH adjusting liquid, the scraped surface heat exchanger adjusts the temperature of the heat exchange outlet to 80-85°C by steam temperature regulation, and the pH adjusting liquid includes citric acid and acetic acid. When the pH is adjusted to 4.0-4.5 (close to the isoelectric point of most phosphorus shrimp proteins), the surface charge of the protein molecules is neutralized, the solubility is significantly reduced, and it is easier to form loose flocculation particles rather than tightly attached scale layers. The scraped surface heat exchanger can easily scrape these particles off the heat exchange surface, reduce the fouling resistance, and keep the heat transfer efficiency stable (15%-30% higher than under neutral conditions). Moreover, the weakly acidic environment with a pH of 4.0-4.5 can minimize the degradation of functional ingredients (such as Omega-3 fatty acids and astaxanthin). Citric acid and acetic acid are food additives allowed by GB2760, which meet the processing requirements of food-grade or health product-grade raw materials.

[0058] In one example, the built-in solution of the flocculation tank 6 has a pH value of 4.0-4.5, and the built-in solution is left to stand for 1.5-2.0 hours before the flocculation tank 6 is used. Therefore, it is more preferable to use multiple flocculation tanks 6 for rotation in this case. Figure 4 In one example, the number of flocculation tanks 6 is 2.

[0059] The flocculation tank 6 comprises a temperature sensor, a PH sensor and a liquid passage pipeline. The temperature sensor can be arranged inside or outside the cylinder wall to detect the temperature of the solution inside the flocculation tank 6. The PH sensor can be arranged inside or outside the cylinder wall to detect the PH value of the solution inside the flocculation tank 6. The liquid passage pipeline is arranged outside the cylinder wall to pass in cooling water or hot water. When the flocculation tank 6 enters the cooling stage, the liquid passage pipeline passes in cooling water. When the flocculation tank enters the heating stage, the liquid passage pipeline passes in hot water. The liquid passage pipeline is made of stainless steel pipeline to pass in cooling water or hot water, and the temperature regulation of the medium inside the flocculation tank is realized by wall heat conduction.

[0060] When the flocculation tank is working, it has the following three stages:

[0061] The first stage is the heat preservation stage. The flocculation tank 6 maintains the temperature of the liquid output by the heat exchanger 5, that is, it maintains 80-85℃. During this period, the temperature sensor continuously detects the temperature of the solution (also known as internal medium) inside the flocculation tank 6. When the detected value is lower than 80℃, the liquid passage pipeline passes in hot water. When the detected value is higher than 85℃, the liquid passage pipeline passes in cooling water. The vacuum degree of this stage ranges from -0.08 to -0.09 MPa (minimum value) to atmospheric pressure (0 MPa) (maximum value). The pulse frequency f is 0.5-1 Hz (30-60 times per minute), and the corresponding single cycle time T is 1-2 s. The duty cycle DC (vacuum time ratio) is 50%-70%, the vacuum holding time T_h is 0.3-0.8 s, and the pressure release time T_v is required to be <0.2 s (fast release). This stage supports stronger vacuum-driven bubble nucleation, high-frequency pulsation enhances disturbance, prolongs vacuum time, strengthens dehydration, and induces cavitation effect by fast pressure release.

[0062] The second stage is the key maturation stage. The flocculation tank 6 is cooled to 60℃ within 5 min and maintained at 60℃ within 30 min. When the detected value is lower than 60℃, the liquid passage pipeline passes in hot water. When the detected value is higher than 60℃, the liquid passage pipeline passes in cooling water. The vacuum degree of this stage ranges from -0.07 to -0.08 MPa (minimum value) to atmospheric pressure (0 MPa) (maximum value). The pulse frequency f is reduced to 0.2-0.5 Hz (12-30 times per minute), and the corresponding single cycle time T_cycle is 2-5 s. The duty cycle DC is 40%-60%, the vacuum holding time T_h is extended to 0.5-1.5 s, and the pressure release time T_v is 0.2-0.5 s. This stage reduces the frequency to reduce the shear force, which is beneficial to the growth of the flocculation body, prolongs the vacuum holding time, promotes the densification of the flocculation body, and slows down the pressure release speed to reduce the disturbance to the flocculation body.

[0063] The third stage, i.e. the promoting settling stage, the flocculation tank 6 is cooled to 45℃ within 5 min and maintained at 45℃ within 30 min. When the detected value is lower than 45℃, the liquid passage is connected to hot water, and when the detected value is higher than 45℃, the liquid passage is connected to cooling water. The vacuum degree range is further adjusted to -0.06~ -0.07 MPa (minimum value) to atmospheric pressure (0 MPa) (maximum value) in this stage. The pulsation frequency f is the lowest, 0.1~0.2 Hz (6~12 times per minute), and the corresponding single cycle time T_c is the longest, 5~10 s. The duty cycle DC is 30%~50%, the vacuum holding time T_h is the longest, 1.0~3.0 s, and the pressure releasing time T_v is the slowest, 0.5~1.0 s. The lowest frequency and the longest cycle time in this stage aim to minimize the shear force, which is conducive to the stable settling of the flocculation; the lowest vacuum degree avoids the destruction of the flocculation structure; and the shortened vacuum time ratio and the slowest pressure releasing are both to minimize the disturbance.

[0064] In one example, the filter 7 is a horizontal microfilter, the filter screen aperture of the horizontal microfilter is 100 μm, and the rotating drum speed of the horizontal microfilter is 15-20 rpm.

[0065] The system performs first three-phase separation on the cooked Antarctic krill solid-liquid mixture to obtain a first solid-phase output and a first liquid-phase output, performs second three-phase separation on the first liquid-phase output and a third liquid-phase output fed by the extruder 3 to obtain a second solid-phase output and a third solid-phase output, and feeds the second solid-phase output fed by the disc centrifuge together with the first solid-phase output to the extruder 3 to obtain the third liquid-phase output and the target Antarctic krill solid product. The system design adopts multiple feedbacks, fully utilizes the raw materials, and improves the utilization rate. The extruder 3 adopts a double-screw extruder 3 to reduce the moisture content of the solid product, avoids the direct passing of the high-moisture solid product through a single-screw pump into a subsequent dryer to cause material caking, simultaneously reduces the moisture content to reduce the heat load of the subsequent dryer and the risk of caking of the dried material, and further extrudes liquid from the extruder 3 to be fed into the disc centrifuge 2 again to separate and obtain crude oil, thereby improving the utilization rate. The solid product (including the first solid-phase output and the second solid-phase output) of the cooked solid-liquid mixture improves the yield of shrimp powder (i.e. the target Antarctic krill solid product).

[0066] Another embodiment of the present application discloses a shipborne three-phase separation recycling method based on the above shipborne three-phase separation recycling system. Referring to Figure 6 the method comprises the following steps:

[0067] In step 601, a cooked Antarctic krill solid-liquid mixture is fed.

[0068] In step 602, the Antarctic krill solid-liquid mixture is subjected to three-phase separation to obtain a first solid-phase output, a first liquid-phase output, and a first oil-phase output.

[0069] Step 603, triphasic separation is performed on the first liquid phase output and the fed third liquid phase output to obtain a second solid phase output and a second liquid phase output; the fed third liquid phase output is generated when the first solid phase output and the second solid phase output are subjected to compression shear dehydration treatment to obtain the target Antarctic krill solid.

[0070] Step 604, heating, flocculation and filtration are performed on the second liquid phase output to obtain the target protein phospholipid complex.

[0071] In one embodiment, step 604, heating, flocculation and filtration are performed on the second liquid phase output to obtain the target protein phospholipid complex, including:

[0072] The PH sensor of the flocculation tank detects the PH value of the built-in solution (also known as internal medium) of the flocculation tank, and according to the PH value, the flocculation tank is fed with a flocculant of corresponding acidity and alkalinity to adjust the PH value of the second liquid phase output to the range of 4.0-4.5, and is left for 1.5-2.0h.

[0073] Hot water or cooling water is introduced into the liquid passage of the flocculation tank to realize temperature control of the second liquid phase output by wall heat conduction, so as to adjust the temperature of the second liquid phase output to the range of 80-85℃, and maintain the temperature for 20min. During the temperature maintaining period, the temperature of the second liquid phase output is maintained at 80-85℃. The vacuum degree in this stage ranges from -0.08 to -0.09MPa (minimum) to atmospheric pressure (0MPa) (maximum). The pulsation frequency f is 0.5-1Hz (30-60 times / minute), and the corresponding single cycle time T is 1-2s. The duty cycle DC (vacuum time ratio) is 50%-70%, the vacuum holding time T_h is 0.3-0.8s, and the pressure release time T_v is required to be <0.2s (fast release). This stage supports stronger vacuum-driven bubble nucleation, high-frequency pulsation enhances disturbance, prolongs vacuum time, strengthens dehydration, and fast pressure release induces cavitation effect.

[0074] The cooling water is continuously fed into the liquid pipeline of the flocculation tank to reduce the temperature of the second liquid phase output to 60°C within 5 minutes, and the cooling water or hot water is fed into the liquid pipeline according to the temperature reduction time of 30 minutes, so that the temperature of the second liquid phase output is maintained at 60°C through wall heat conduction, and the flocculation network of the flocculation material in the second liquid phase output is promoted to expand. The vacuum degree in this stage ranges from -0.07 to -0.08 MPa (minimum value) to atmospheric pressure (0 MPa) (maximum value). The pulsation frequency f is reduced to 0.2-0.5 Hz (12-30 times / minute), and the corresponding single cycle time T cycle is 2-5 s. The duty cycle DC is 40%-60%, the vacuum holding time T h is extended to 0.5-1.5 s, and the pressure release time T v is 0.2-0.5 s. The frequency is reduced in this stage to reduce the shear force, facilitate the growth of the flocculation body, extend the vacuum holding time, promote the densification of the flocculation body, and slow down the pressure release speed to reduce the disturbance to the flocculation body.

[0075] The cooling water is continuously fed into the liquid pipeline of the flocculation tank to reduce the temperature of the second liquid phase output to 60°C within 5 minutes, and the cooling water or hot water is fed into the liquid pipeline according to the temperature reduction time of 30 minutes, so that the temperature of the second liquid phase output is maintained at 60°C through wall heat conduction, and the flocculation network of the flocculation material in the second liquid phase output is promoted to expand. The vacuum degree in this stage ranges from -0.07 to -0.08 MPa (minimum value) to atmospheric pressure (0 MPa) (maximum value). The pulsation frequency f is reduced to 0.2-0.5 Hz (12-30 times / minute), and the corresponding single cycle time T cycle is 2-5 s. The duty cycle DC is 40%-60%, the vacuum holding time T h is extended to 0.5-1.5 s, and the pressure release time T v is 0.2-0.5 s. The frequency is reduced in this stage to reduce the shear force, facilitate the growth of the flocculation body, extend the vacuum holding time, promote the densification of the flocculation body, and slow down the pressure release speed to reduce the disturbance to the flocculation body.

[0076] The flocculation slurry from each flocculation tank is separated by a filter to filter out water to extract the target protein phospholipid complex.

[0077] The above are preferred embodiments of the present application, which do not limit the protection scope of the present application, and therefore: any equivalent changes made according to the structure, shape, principle of the present application should be covered within the protection scope of the present application.

Claims

1. A shipborne three-phase separation and recycling system for the solid-liquid mixture of Antarctic krill obtained through cooking and separation, characterized in that, The system includes a horizontal screw centrifuge, a disc centrifuge, an extruder, and a heat exchange flocculation assembly; The horizontal screw centrifuge performs three-phase separation on the fed Antarctic krill solid-liquid mixture to obtain a first solid phase output, a first liquid phase output, and a first oil phase output; The disc centrifuge is connected to the horizontal screw centrifuge, the extruder, and the heat exchange flocculation assembly. The disc centrifuge performs three-phase separation on the first liquid phase output and the third liquid phase output from the extruder, and the second oil phase output is divided into a second solid phase output, a second liquid phase output, and a second oil phase output. The extruder is connected to the horizontal screw centrifuge and the disc centrifuge to perform compression, shearing and dehydration treatment on the first solid output and the second solid output to obtain the target Antarctic krill solid and the third liquid output. The heat exchange flocculation component is connected to the disc centrifuge to heat, flocculate, and filter the second liquid phase output to obtain the target protein phospholipid complex.

2. The system according to claim 1, characterized in that, The heat exchange flocculation assembly includes a heat exchanger, a filter, and at least one flocculation tank; The heat exchanger is connected to the disc centrifuge to internally heat the second liquid phase output to meet the target protein coagulation temperature conditions. The at least one flocculation tank is connected to the heat exchanger to perform uniform flocculation treatment on the heated second liquid phase output to obtain flocculated slurry. The filter is connected to at least one flocculation tank to separate the flocculated slurry and extract the target protein phospholipid complex.

3. The system according to claim 1, characterized in that, The system also includes an output pump connected to the extruder to deliver the target Antarctic krill solids.

4. The system according to claim 1, characterized in that, The horizontal screw centrifuge has a first feed inlet, a first solid phase output inlet, a first liquid phase output inlet and a first oil phase output inlet; the disc centrifuge has a second feed inlet, a second solid phase output inlet, a second liquid phase output inlet and a second oil phase output inlet; and the extruder has a third feed inlet, a third solid phase output inlet and a third liquid phase output inlet. The first feed port is used to feed the Antarctic krill solid-liquid mixture. The first solid phase output port and the second solid phase output port are both connected to the third feed port to transfer the first solid phase output and the second solid phase output. The second liquid phase output port and the third liquid phase output port are both connected to the second feed port to transfer the first liquid phase output and the third liquid phase output. The first oil phase output port is used to output the first oil phase output. The second liquid phase outlet is connected to the heat exchange flocculation component to transmit the second liquid phase output, and the second oil phase outlet is used to output the second oil phase output. The third solid output port is used to output the target Antarctic krill solids.

5. The system according to claim 1, characterized in that, The horizontal screw centrifuge has a rotational speed of 4500 rpm, the disc centrifuge has a rotational speed of 10000 rpm, the extruder is a twin-screw extruder, the screen aperture of the twin-screw extruder is 0.5-1.0 mm, the compression ratio of the twin-screw extruder is 6:1, and the rotational speed of the twin-screw extruder is 100 rpm.

6. The system according to claim 2, characterized in that, The heat exchanger is a scraped heat exchanger. The pH value of the built-in solution in the flocculation tank is 4.0-4.

5. The built-in solution is allowed to stand for 1.5-2.0 hours before the flocculation tank is put into operation. The filter is a horizontal microfilter with a filter screen pore size of 100μm and a drum speed of 15-20rpm.

7. The system according to claim 6, characterized in that, The scraped heat exchanger is equipped with a pH regulator at the heat exchange inlet. The pH regulator injects a pH adjusting liquid to make the pH value of the second liquid phase output injected into the scraped heat exchanger 4.0-4.

5. The scraped heat exchanger adjusts the temperature of the heat exchange outlet to 80-85℃ by steam temperature regulation. The pH adjusting liquid includes citric acid and acetic acid.

8. The system according to claim 6, characterized in that, The flocculation tank includes a temperature sensor, a pH sensor, and a liquid-passing pipe disposed on the outside of the tank wall. The temperature sensor is used to detect the temperature of the built-in solution, the pH sensor is used to detect the pH value of the built-in solution, and the liquid-passing pipe is used to pass cooling water or hot water through it.

9. A shipborne three-phase separation and recycling method, characterized in that, Based on the shipborne three-phase separation and recycling system according to any one of claims 1-7, the method includes: A solid-liquid mixture of Antarctic krill obtained by separation after feeding and cooking; The Antarctic krill solid-liquid mixture was subjected to three-phase separation to obtain a first solid phase output, a first liquid phase output, and a first oil phase output; The first liquid phase output and the third liquid phase output are subjected to three-phase separation to obtain a second solid phase output and a second liquid phase output; the third liquid phase output is generated when the first solid phase output and the second solid phase output are subjected to compression shear dehydration treatment to obtain the target Antarctic krill solids; The second liquid phase output is heated, flocculated, and filtered to obtain the target protein phospholipid complex.

10. The method according to claim 9, characterized in that, The process of heating, flocculating, and filtering the second liquid phase output to obtain the target protein phospholipid complex includes: Adjust the pH of the second liquid phase output to the range of 4.0-4.5, and heat the second liquid phase output to 80-85℃; Based on a heat preservation time of 20 minutes, maintain the temperature of the second liquid phase output at 80-85℃; The temperature of the second liquid phase output is reduced to 60°C within 5 minutes, and the temperature of the second liquid phase output is maintained at 60°C for a cooling time of 30 minutes to promote the expansion of the flocculation network of flocculants in the second liquid phase output. The temperature of the second liquid phase output is further reduced to 45°C within 5 minutes, and the temperature of the second liquid phase output is maintained at 45°C according to the promotion time of 30 minutes, so as to promote the compaction of the flocculants and form flocculent slurry. The flocculated slurry was separated to extract the target protein phospholipid complex.

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